Classifications

• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
  • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
  • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
  • C01B3/58—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids including a catalytic reaction
  • C01B3/583—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids including a catalytic reaction the reaction being the selective oxidation of carbon monoxide
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
  • B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
  • B01J23/56—Platinum group metals
  • B01J23/58—Platinum group metals with alkali- or alkaline earth metals
• • H—ELECTRICITY
  • H01—ELECTRIC ELEMENTS
  • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
  • H01M8/00—Fuel cells; Manufacture thereof
  • H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
  • H01M8/0662—Treatment of gaseous reactants or gaseous residues, e.g. cleaning
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
  • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
  • C01B2203/0435—Catalytic purification
  • C01B2203/044—Selective oxidation of carbon monoxide
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
  • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
  • C01B2203/0465—Composition of the impurity
  • C01B2203/047—Composition of the impurity the impurity being carbon monoxide
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
  • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
  • Y02E60/30—Hydrogen technology
  • Y02E60/50—Fuel cells

Definitions

• the present invention relates to a carbon monoxide concentration reducing device, a carbon monoxide concentration reducing method, and a carbon monoxide selective oxidation catalyst. More specifically, the present invention relates to a carbon monoxide concentration reducing device that reduces the concentration of carbon monoxide in a hydrogen-rich gas. The present invention relates to a method for reducing the concentration of carbon monoxide and a selective oxidation catalyst for carbon monoxide. Background art
• a device for reducing the concentration of carbon monoxide in a hydrogen-rich gas there has been proposed a device provided with a catalyst made of ruthenium supported on a carrier such as alumina (for example, Japanese Unexamined Patent Publication No. Hei 8-133701, Japanese Unexamined Patent Publication No. Hei 8-133702, Japanese Unexamined Patent Publication No. Hei 8-217406, etc.).
• a catalyst made of ruthenium promotes a selective oxidation reaction of carbon monoxide, which oxidizes carbon monoxide in preference to an oxidation reaction of hydrogen.
• the carbon concentration can be reduced.
• Such a carbon monoxide concentration reducing device is used, for example, in a fuel cell device including a polymer electrolyte fuel cell and a phosphoric acid fuel cell.
• a fuel cell device including a polymer electrolyte fuel cell and a phosphoric acid fuel cell. The following shows the electrochemical reactions that occur in these fuel cells.
• Equation (1) shows the reaction on the anode side of the fuel cell
• equation (2) shows the reaction on the force side of the fuel cell
• equation (3) shows the reaction performed on the whole cell.
• the anode side It is necessary to supply a fuel gas containing hydrogen to the fuel cell and an oxidizing gas containing oxygen to the cathode side. At this time, if carbon monoxide is mixed in these gases, the mixed carbon monoxide is adsorbed on the platinum catalyst provided in the fuel cell, and the function as a catalyst is reduced.
• the oxidizing gas Normally, air or the like is used as the oxidizing gas.Therefore, there is no danger that the amount of carbon monoxide that degrades the catalytic function is mixed in the oxidizing gas, but a small amount of carbon monoxide is mixed in the fuel gas. Therefore, the decomposition reaction of hydrogen that proceeds on the anode side may be hindered, and the performance of the fuel cell may be reduced.
• a fuel cell system using such a reformed gas as a fuel gas to be supplied to a fuel cell usually includes a predetermined fuel reforming device.
• the fuel reforming device reforms hydrocarbons to form a hydrogen rich.
• the fuel gas is generated and supplied to the anode side of the fuel cell.
• a reaction for steam reforming of methanol is shown below.
• the reverse shift reaction shown in equation (7) is a reaction that produces carbon monoxide from hydrogen and carbon dioxide generated by the steam reforming reaction.
• This reverse shift reaction proceeds very little in comparison to the steam reforming reaction, but the concentration of carbon monoxide is extremely low, as in the case of using the reformed gas as the fuel gas supplied to the fuel cell. If required, carbon monoxide generated by the reverse shift reaction may have a significant effect. Therefore, when supplying the fuel gas to the fuel cell, the concentration of carbon monoxide in the fuel gas has been reduced by the carbon monoxide concentration reducing device.
• the selective oxidation reaction of carbon monoxide that oxidizes carbon monoxide in preference to hydrogen contained in a large amount in the reformed gas proceeds.
• the oxidation reaction of carbon monoxide is shown in the following equation (8).
• the allowable concentration of carbon monoxide in the fuel gas supplied to the fuel cell is generally about several percent or less in the case of a phosphoric acid fuel cell, and in the case of a polymer electrolyte fuel cell. It is said to be less than a few Ppm.
• the reformed gas is supplied to the carbon monoxide concentration reduction device equipped with the ruthenium catalyst described above, and the selective oxidation reaction of carbon monoxide represented by the following equation (8) is advanced. It is possible to reduce the carbon oxide concentration and supply fuel gas with a sufficiently low carbon monoxide concentration to the fuel cell.
• the above-mentioned ruthenium catalyst has a temperature range enough to promote the selective oxidation reaction of carbon monoxide at about 140 to 200 ° C, and a carbon monoxide concentration reduction device equipped with a ruthenium catalyst has already been described.
• concentration of carbon monoxide in the fuel gas supplied to the fuel cell was reduced by incorporating it into the fuel cell device, the concentration of carbon monoxide in the fuel gas could not be sufficiently reduced.
• the temperature in the carbon monoxide concentration reduction device falls below the effective temperature range described above, the oxidation activity of the catalyst decreases, and the oxidation reaction of carbon monoxide becomes difficult to proceed, and the carbon monoxide concentration decreases sufficiently. It will not be done.
• the temperature in the carbon monoxide concentration reduction device is higher than the effective temperature range described above, hydrogen abundantly present in the fuel gas is oxidized and mixed.
• the selective oxidation of a trace amount of carbon monoxide becomes difficult, and the oxidation reaction of carbon monoxide cannot be sufficiently performed. Therefore, in order to sufficiently reduce the concentration of carbon monoxide, the internal temperature of the carbon monoxide concentration reduction device is controlled according to the amount of reformed gas used for the selective oxidation reaction of carbon monoxide, and the carbon monoxide is selected.
• the oxidation reaction must proceed within the effective temperature range described above.
• the internal temperature of the carbon monoxide concentration reduction device is set to a predetermined temperature range. May be difficult to maintain.
• the load fluctuates drastically, and a carbon monoxide concentration reduction device is used with the load fluctuation.
• the amount of reformed gas to be treated also fluctuates greatly, making it difficult to control the internal temperature of the carbon monoxide concentration reduction device.
• the internal temperature may rise too rapidly.
• the load suddenly decreases and the amount of treatment in the carbon monoxide concentration reduction device decreases accordingly, the internal temperature may drop too rapidly.
• the internal temperature of the carbon monoxide concentration reducing device deviates from the above-mentioned desirable temperature range due to the load fluctuation, the above-described inconvenience occurs, and the carbon monoxide concentration in the reformed gas is reduced. The reduction cannot be performed effectively. Therefore, when the load fluctuation of the fuel cell is large to some extent, in order to maintain the activity of the selective oxidation reaction of carbon monoxide sufficiently, the effective temperature range of the carbon monoxide selective oxidation catalyst must be wider. desirable.
• the operating temperature range of the fuel cell that receives the supply of the fuel gas from the carbon monoxide concentration reduction device is about 80 to 100 ° C in the case of the above-described polymer electrolyte fuel cell, and the carbon monoxide If the temperature of the fuel gas supplied from the concentration reduction device to the fuel cell is higher than the operating temperature of the fuel cell, the fuel gas supplied from the carbon monoxide concentration reduction device is directly supplied to the fuel cell. Temperature rises to an undesired temperature, causing inconvenience.
• the temperature of the oxidation reaction in the carbon monoxide concentration reduction device (the temperature at which the carbon monoxide selective oxidation catalyst can sufficiently promote the reaction) If the controlled temperature exceeds the operating temperature range of the fuel cell, a predetermined heat exchange means is provided in a fuel gas flow path connecting the carbon monoxide concentration reducing device and the fuel cell, and Prior to supplying the battery, it was necessary to sufficiently lower the temperature of the fuel gas in advance. Provision of such a heat exchange means caused inconveniences such as complicated piping and a large-sized device.
• the catalyst that promotes the selective oxidation reaction of carbon monoxide has a wider temperature range in which the selective oxidation reaction of carbon monoxide can be sufficiently promoted in order to sufficiently cope with load fluctuation.
• the low temperature side of the temperature range is closer to the operating temperature of the fuel cell.
• the low temperature side of the temperature range in which the carbon monoxide concentration can be sufficiently reduced is about 140 ° C. as described above, which is the operating temperature of the fuel cell. In the temperature range of about 0 ° C, the selective oxidation reaction of carbon monoxide could not be sufficiently promoted.
• the carbon monoxide concentration reducing device, the carbon monoxide concentration reducing method, and the carbon monoxide selective oxidation catalyst of the present invention solve these problems and broaden the temperature range in which the activity of the carbon monoxide selective oxidation reaction becomes sufficiently high.
• the objective is to bring the lower end of the sufficiently high temperature range closer to the operating temperature of the fuel cell. Disclosure of the invention
• the first carbon monoxide concentration reducing device of the present invention is a first carbon monoxide concentration reducing device of the present invention.
• a carbon monoxide concentration reducing device that reduces the concentration of carbon monoxide by oxidizing carbon monoxide contained in a hydrogen-rich gas
• Hydrogen rich gas supply means for supplying the hydrogen rich gas
• Oxidizing gas supply means for supplying an oxidizing gas containing oxygen used for oxidizing the carbon monoxide
• a selective oxidation catalyst for carbon monoxide for selectively oxidizing carbon monoxide comprising a selective oxidation catalyst for carbon monoxide having ruthenium as a main component, wherein the hydrogen rich gas supply means and the oxidizing gas supply means The hydrogen rich gas and the oxidizing gas are supplied, and the hydrogen rich gas is supplied by the carbon monoxide selective oxidation reaction.
• the gist of the present invention is to further include a metal element having an effect of increasing the temperature range.
• the first apparatus for reducing the concentration of carbon monoxide of the present invention configured as described above receives the supply of the hydrogen rich gas and the oxidizing gas from the hydrogen rich gas supplying means and the oxidizing gas supplying means, respectively,
• carbon selective oxidation reaction carbon monoxide contained in the hydrogen rich gas is selectively oxidized to reduce the concentration of the carbon monoxide.
• the selective oxidation of carbon monoxide is further provided in addition to ruthenium as a main component, an alkali metal element having an effect of increasing the temperature range in which the selective oxidation reaction of carbon monoxide can be promoted.
• the selective oxidation reaction of carbon monoxide is advanced using a catalyst.
• a selective oxidation catalyst for carbon monoxide that promotes a selective oxidation reaction of carbon monoxide for selectively oxidizing carbon monoxide and has ruthenium as a main component, in a temperature range in which the selective oxidation reaction of carbon monoxide can be promoted.
• the gist consists of
• a carbon monoxide selective oxidation catalyst for promoting a carbon monoxide selective oxidation reaction for selectively oxidizing carbon monoxide contained in hydrogen rich gas
• Ruthenium which is the main component is supported on a predetermined carrier
• the temperature range in which the selective oxidation reaction of carbon monoxide can be promoted further increases.
• the concentration of carbon monoxide in the hydrogen-rich gas can be sufficiently reduced in a wider temperature range. Therefore, when the concentration of carbon monoxide in the hydrogen-rich gas is reduced, the operation of controlling the temperature of the carbon monoxide selective oxidation catalyst becomes easier so that the temperature range is such that the concentration of carbon monoxide is sufficiently reduced. .
• the treatment amount (the amount of hydrogen littigas supplied to the carbon monoxide concentration reducing device) varies in the carbon monoxide concentration reducing device of the present invention, for example, the carbon monoxide concentration is reduced by the carbon monoxide concentration reducing device.
• the hydrogen rich gas with reduced amount is supplied as a fuel gas to a fuel cell in which the connected load varies. That is, if the amount of hydrogen rich gas whose carbon monoxide concentration should be reduced fluctuates, the amount of heat generated by the carbon monoxide selective oxidation reaction fluctuates, and the temperature of the carbon monoxide selective oxidation catalyst rises and falls. Even if the catalyst temperature changes, the temperature range in which the concentration of carbon monoxide is sufficiently reduced is wide, so that a state in which the concentration of carbon monoxide is sufficiently reduced can be stably maintained.
• the alkali metal element may be provided as a simple substance on the predetermined carrier.
• the alkali metal element and the ruthenium may be supported on the predetermined carrier in the form of an alloy.
• the carbon monoxide concentration reducing apparatus, the carbon monoxide concentration reducing method, and the carbon monoxide selective oxidation catalyst of the present invention are supported on the predetermined carrier in the form of an alloy.
• the alkali metal element may be any one of lithium and potassium.
• the temperature range in which the selective oxidation reaction of carbon monoxide can be promoted can be expanded particularly to the low temperature side. it can. Therefore, when a hydrogen rich gas having a reduced carbon monoxide concentration is supplied as a fuel gas to a polymer electrolyte fuel cell, for example, the hydrogen rich gas having a reduced carbon monoxide concentration is supplied to the fuel cell. Prior to this, the step of lowering the temperature of the hydrogen rich gas can be simplified or omitted.
• the second carbon monoxide concentration reducing device of the present invention comprises:
• a carbon monoxide concentration reducing device that reduces the concentration of carbon monoxide by oxidizing carbon monoxide contained in a hydrogen-rich gas
• Hydrogen rich gas supply means for supplying the hydrogen rich gas
• Oxidizing gas supply means for supplying an oxidizing gas containing oxygen used for oxidizing the carbon monoxide
• a selective oxidation catalyst for carbon monoxide for selectively oxidizing carbon monoxide comprising a selective oxidation catalyst for carbon monoxide having ruthenium as a main component, wherein the hydrogen rich gas supply means and the oxidizing gas supply means
• a carbon monoxide selective oxidation reaction unit that receives supply of a hydrogen rich gas and the oxidizing gas and selectively oxidizes carbon monoxide contained in the hydrogen-rich gas by the carbon monoxide selective oxidation reaction;
• the gist of the present invention is that the carbon selective oxidation catalyst further includes an alkaline earth metal element having an effect of increasing the temperature range in which the carbon monoxide selective oxidation reaction can be promoted by being used together with ruthenium.
• the second carbon monoxide concentration reducing apparatus of the present invention configured as described above receives the supply of the hydrogen rich gas and the oxidizing gas from the hydrogen rich gas supply means and the oxidizing gas supply means, respectively, By the carbon selective oxidation reaction, It selectively oxidizes carbon monoxide contained in hydrogen rich gas to reduce the concentration of the carbon monoxide.
• the carbon monoxide further includes, in addition to ruthenium as a main component, an alkaline earth metal element having an effect of increasing a temperature range in which the selective oxidation reaction of carbon monoxide can be promoted by being used together with ruthenium.
• ruthenium as a main component
• an alkaline earth metal element having an effect of increasing a temperature range in which the selective oxidation reaction of carbon monoxide can be promoted by being used together with ruthenium.
• a selective oxidation catalyst for carbon monoxide that promotes a selective oxidation reaction of carbon monoxide for selectively oxidizing carbon monoxide and has ruthenium as a main component, in a temperature range in which the selective oxidation reaction of carbon monoxide can be promoted.
• the gist consists of
• a carbon monoxide selective oxidation catalyst that promotes a carbon monoxide selective oxidation reaction for selectively oxidizing carbon monoxide contained in hydrogen rich gas
• Ruthenium which is the main component is supported on a predetermined carrier
• the temperature range in which the selective oxidation of carbon monoxide can be promoted further increases.
• the concentration of carbon monoxide in the hydrogen-rich gas can be sufficiently reduced in a wider temperature range. Therefore, the first apparatus for reducing the concentration of carbon monoxide of the present invention.
• the operation of controlling the temperature of the selective oxidation catalyst for carbon monoxide becomes easier, and the amount of hydrogen rich gas that should reduce the concentration of carbon monoxide fluctuates.
• the temperature range in which the concentration of carbon monoxide is sufficiently reduced is wide, it is possible to stably maintain the state in which the concentration of carbon monoxide is sufficiently reduced.
• the alkaline earth metal element may be provided on the predetermined carrier as a simple substance.
• the alkaline earth metal element and the ruthenium may be supported on the predetermined carrier in the form of an alloy.
• the alkaline earth metal may be barium.
• the temperature range in which the carbon monoxide selective oxidation reaction can be promoted can be extended to a lower temperature side. it can. Therefore, when a hydrogen rich gas having a reduced carbon monoxide concentration is supplied as a fuel gas to a polymer electrolyte fuel cell, for example, the hydrogen rich gas having a reduced carbon monoxide concentration is supplied to the fuel cell. Previously, the step of lowering the temperature of the hydrogen rich gas can be simplified or omitted.
• the third device for reducing the concentration of carbon monoxide of the present invention comprises:
• a carbon monoxide concentration reducing device that reduces the concentration of carbon monoxide by oxidizing carbon monoxide contained in hydrogen rich gas
• Hydrogen rich gas supply means for supplying the hydrogen rich gas
• a hydrogen-rich gas supply comprising a carbon monoxide selective oxidation catalyst that promotes a carbon monoxide selective oxidation reaction for selectively oxidizing carbon monoxide and has ruthenium as a main component; Means for receiving the supply of the hydrogen rich gas and the oxidizing gas from the means and the means for supplying the oxidizing gas, respectively, and selectively oxidizing carbon monoxide contained in the hydrogen-rich gas by the selective oxidation reaction of carbon monoxide.
• a selective oxidation reaction section, wherein the carbon monoxide selective oxidation catalyst further comprises nickel.
• the third carbon monoxide concentration reducing device of the present invention configured as described above receives the supply of the hydrogen rich gas and the oxidizing gas from the hydrogen rich gas supply unit and the oxidizing gas supply unit, respectively, By carbon selective oxidation reaction, carbon monoxide contained in the hydrogen rich gas is selectively oxidized to reduce the concentration of the carbon monoxide. At this time, the carbon monoxide selective oxidation reaction is advanced using a carbon monoxide selective oxidation catalyst further comprising nickel in addition to ruthenium as a main component. Further, the third method of reducing the concentration of carbon monoxide of the present invention,
• a selective oxidation catalyst for carbon monoxide which promotes a selective oxidation reaction of carbon monoxide for selectively oxidizing carbon monoxide, and comprises a catalyst for selectively oxidizing carbon monoxide having ruthenium as a main component, wherein the catalyst further comprises nickel. Reducing the concentration of carbon monoxide in the hydrogen rich gas mixed with the oxidizing gas by a carbon selective oxidation reaction;
• the gist consists of
• a carbon monoxide selective oxidation catalyst for promoting a carbon monoxide selective oxidation reaction for selectively oxidizing carbon monoxide contained in hydrogen rich gas
• Ruthenium which is the main component is supported on a predetermined carrier
• the gist is to further include nickel.
• the method for reducing the concentration of carbon monoxide and the selective oxidation catalyst for carbon monoxide of the present invention the temperature range in which the selective oxidation of carbon monoxide can be promoted further increases. Compared with the case of using a conventionally known ruthenium catalyst Furthermore, the carbon monoxide concentration in the hydrogen-rich gas can be sufficiently reduced over a wider temperature range. Therefore, as in the case of the first and second carbon monoxide concentration reducing devices, the carbon monoxide concentration reducing method, and the carbon monoxide selective oxidation catalyst of the present invention, the operation of controlling the temperature of the carbon monoxide selective oxidation catalyst is performed.
• the temperature range in which the carbon monoxide concentration is sufficiently reduced is wide, so the carbon monoxide concentration is sufficiently reduced. This has the effect of maintaining a stable state.
• the temperature range in which the selective oxidation reaction of carbon monoxide can be promoted can be expanded particularly to a lower temperature side. Therefore, when supplying a hydrogen rich gas having a reduced carbon monoxide concentration as a fuel gas to, for example, a polymer electrolyte fuel cell, the temperature of the hydrogen rich gas having a reduced carbon monoxide concentration is supplied to the fuel cell. Prior to this, the step of lowering the temperature of the hydrogen rich gas can be simplified or omitted.
• the fourth device for reducing the concentration of carbon monoxide of the present invention comprises:
• a carbon monoxide concentration reducing device that reduces the concentration of carbon monoxide by oxidizing carbon monoxide contained in a hydrogen-rich gas
• Hydrogen rich gas supply means for supplying the hydrogen rich gas
• a selective oxidation catalyst for carbon monoxide for selectively oxidizing carbon monoxide a selective oxidation catalyst for carbon monoxide having ruthenium as a main component; wherein the hydrogen-rich gas supply means and the oxidant gas supply means A carbon monoxide selective oxidation reaction unit that receives supply of a hydrogen rich gas and the oxidizing gas and selectively oxidizes carbon monoxide contained in the hydrogen-rich gas by the carbon monoxide selective oxidation reaction;
• the gist of the present invention is that the carbon selective oxidation catalyst further includes zinc.
• the fourth carbon monoxide concentration reducing device of the present invention configured as described above receives the hydrogen rich gas and the oxidizing gas from the hydrogen rich gas supplying unit and the oxidizing gas supplying unit, respectively.
• carbon selective oxidation reaction carbon monoxide contained in the hydrogen rich gas is selectively oxidized, and the concentration of the carbon monoxide is increased.
• the carbon monoxide selective oxidation reaction is advanced using a carbon monoxide selective oxidation catalyst further comprising zinc in addition to ruthenium as a main component.
• the fourth method for reducing the concentration of carbon monoxide of the present invention comprises:
• a method for reducing the concentration of carbon monoxide by oxidizing carbon monoxide contained in a hydrogen-rich gas comprising:
• a carbon monoxide selective oxidation catalyst that promotes a carbon monoxide selective oxidation reaction for selectively oxidizing carbon monoxide, and that includes ruthenium as a main component, wherein the catalyst further comprises zinc; Reducing the concentration of carbon monoxide in the hydrogen rich gas mixed with the oxidizing gas by a selective oxidation reaction;
• the gist consists of
• a carbon monoxide selective oxidation catalyst for promoting a carbon monoxide selective oxidation reaction for selectively oxidizing carbon monoxide contained in hydrogen rich gas
• Ruthenium which is the main component is supported on a predetermined carrier
• the gist is to further include zinc.
• the temperature range in which the selective oxidation reaction of carbon monoxide can be promoted further increases.
• the concentration of carbon monoxide in the hydrogen-rich gas can be sufficiently reduced in a wider temperature range. Therefore, as in the case of the first to third carbon monoxide concentration reducing devices, the carbon monoxide concentration reducing method, and the carbon monoxide selective oxidation catalyst of the present invention, the operation of controlling the temperature of the carbon monoxide selective oxidation catalyst is performed.
• the temperature range in which the carbon monoxide concentration is sufficiently reduced is wide, so the carbon monoxide concentration is sufficiently reduced. This has the effect of maintaining a stable state.
• the temperature range in which the selective oxidation reaction of carbon monoxide can be promoted can be expanded particularly to a lower temperature side. Therefore, carbon monoxide concentration
• the hydrogen when supplying a hydrogen rich gas having a reduced hydrogen content as a fuel gas to a polymer electrolyte fuel cell, before supplying the temperature of the hydrogen rich gas having a reduced carbon monoxide concentration to the fuel cell, the hydrogen The step of lowering the temperature of the rich gas can be simplified or omitted.
• FIG. 1 is a process diagram showing a method for producing a lithium-added ruthenium catalyst
• FIG. 2 is an explanatory diagram schematically showing the configuration of the fuel cell device 10
• FIG. 3 is a schematic cross-sectional view showing the outline of the configuration of a single cell 28 constituting the fuel cell 20
• FIG. 4 is an explanatory view schematically showing the configuration of the CO selective oxidizing section 34
• FIG. 5 is an explanatory diagram showing the results of comparing the performance as a catalyst at various temperatures of a carbon monoxide selective oxidation catalyst comprising ruthenium and a second element of the present invention and a conventionally known ruthenium catalyst.
• FIG. 1 is a process diagram showing a method for producing a lithium-added ruthenium catalyst corresponding to the main part of the present invention
• FIG. 2 is a fuel cell device 10 having a carbon monoxide concentration reduction device provided with the above-mentioned lithium-added ruthenium catalyst.
• FIG. 2 is an explanatory diagram showing an outline of the configuration of FIG.
• the selective oxidation catalyst for carbon monoxide used in this example is a catalyst in which ruthenium and a smaller amount of lithium than ruthenium are supported on alumina pellets.
• the carbon oxide selective oxidation catalyst will be referred to as a lithium-added ruthenium catalyst.
• the activity of promoting the selective oxidation reaction of carbon monoxide is excellent not only at the high temperature side but also at the low temperature side. Therefore, even if the load connected to the fuel cell fluctuates, the concentration of carbon monoxide in the hydrogen rich gas can be sufficiently reduced.
• a method for producing a lithium-added ruthenium catalyst will be described with reference to FIG. 1, and then a fuel cell will be described with reference to FIG. The configuration of the device 10 and the carbon monoxide concentration reduction reaction in the hydrogen-rich gas performed in the fuel cell device 10 will be described.
• an alumina pellet which is a porous body having a particle size of about 3 mm, is prepared, and the aluminum pellet is immersed in distilled water.
• an aqueous lithium acetate solution was prepared separately, and while stirring the distilled water in which the alumina pellet was immersed, the aqueous lithium acetate solution was gradually dropped into the aqueous solution to absorb the lithium salt into the alumina. (Step S110).
• Step S120 the alumina pellet on which the lithium salt was adsorbed was dried to remove water (step S120), and the alumina pellet was heated at 200 ° C for about 1 hour to remove the lithium-supporting pellet.
• Manufacturing Step S130.
• lithium was thus carried on the alumina pellets at a rate of 0.005 mol Z liters (moles of lithium carried per volume of alumina pellets).
• this lithium-supporting pellet is subjected to the same treatment as the above-described treatment for supporting lithium, and further, ruthenium is supported.
• the lithium-supporting pellet is immersed in distilled water (step S140).
• an aqueous ruthenium chloride solution is prepared, and while stirring the distilled water obtained by immersing the above-mentioned lithium-supporting pellet, the aqueous ruthenium chloride solution is gradually dropped into the distilled water so that the ruthenium salt is adsorbed on the alumina (Ste S 150).
• the lithium-supported pellet on which the ruthenium salt has been adsorbed is dried to remove water (step S160).
• the lithium-supported pellet is heated at 500 ° C. for about 2 hours in a hydrogen reducing atmosphere.
• the ruthenium on the pellet is reduced to complete the lithium-added ruthenium catalyst.
• ruthenium was thus loaded on the lithium-carrying pellets at a rate of 0.036 mol Z liters (moles of supported ruthenium per volume of alumina pellets). .
• lithium acetate is used for supporting lithium, but another salt may be used.
• a salt used for supporting ruthenium on the alumina pellet.
• a salt other than ruthenium chloride may be used.
• it can be arbitrarily selected from ruthenium nitrate, ruthenium iodide, ruthenic chloride, ammonium ruthenate, ruthenium hydroxide, potassium ruthenate, or a combination of two or more of these salts. It may be that.
• the fuel cell device 10 includes a methanol tank 12, a water tank 14, a fuel reformer 30, and a fuel cell 20.
• the methanol tank 12 stores methanol
• the water tank 14 stores water, and supplies methanol and water to the fuel reformer 30 via a predetermined supply path.
• the fuel reformer 30 generates a fuel gas containing hydrogen from the supplied methanol and water.
• the fuel cell 20 receives the supply of the fuel gas generated by the fuel reformer 30 and the oxidizing gas containing oxygen to perform an electrochemical reaction to obtain an electromotive force.
• the fuel cell 20 is a polymer electrolyte fuel cell, and has a stack structure in which a plurality of single cells are stacked.
• FIG. 3 is a cross-sectional view schematically illustrating a configuration of a single cell 28 included in the fuel cell 20.
• the unit cell 28 is composed of an electrolyte membrane 21, an anode 22, a power source 23, and separators 24, 25.
• the anode 22 and the power source 23 are gas diffusion electrodes having a sandwich structure with the electrolyte membrane 21 sandwiched from both sides.
• the separators 24 and 25 form a fuel gas and oxidizing gas flow path between the anode 22 and the power source 23 while further sandwiching the San German structure from both sides.
• a fuel gas flow path 24 P is formed between the anode 22 and the separator 24, and an oxidizing gas flow path 25 P is formed between the power source 23 and the separator 25. Have been.
• the electrolyte membrane 2 ⁇ is a proton-conductive ion exchange membrane formed of a solid polymer material, for example, a fluorine-based resin, and has platinum or platinum and another metal as a catalyst on its surface. Is applied.
• the anode 22 and the cathode 23 are made of carbon cloth woven from carbon fiber yarn or carbon fiber Formed of carbon paper or carbon felt.
• the separators 24 and 25 are formed of a gas-impermeable conductive member, for example, dense carbon which is made gas-impermeable by compressing carbon, and has ribs of a predetermined shape formed on its surface. are doing.
• These ribs form a fuel gas flow channel 24 P and an oxidizing gas flow channel 25 P with the surface of the anode 22 or the surface of the force source 23, respectively.
• the separators 24 and 25 are described separately.However, in an actual fuel cell 20, separators having ribs formed on both sides are used, and the adjacent unit cells 28 are used as separators. The configuration was shared.
• the configuration of the single cell 28 which is the basic structure of the fuel cell 20 has been described above.
• a separator is arranged between the configuration composed of the anode 22, the electrolyte membrane 21, and the force source 23, and a plurality of single cells 28 are stacked (in this embodiment, 1
• the stack structure is formed by disposing a current collecting plate composed of dense carbon or a copper plate at both ends.
• FIG. 1 shows only the supply system of the fuel gas supplied to the anode side of the fuel cell 20, an oxidizing gas supply device (not shown) is connected to the cathode side. Pressurized air is supplied. Further, a fuel gas discharge device and an oxidizing gas discharge device (not shown) are connected to the fuel cell 20, and the fuel exhaust gas and the oxidizing exhaust gas after being subjected to the electrochemical reaction at each electrode are discharged from the fuel cell 20. It is discharged outside.
• the fuel reformer 30 includes a reformer 32, a CO selective oxidizer 34, a carbon monoxide sensor 40, a blower 38, and a controller 70 as main components.
• the reforming section 32 receives the supply of methanol and water and generates a hydrogen-rich reformed gas.
• the CO selective oxidizing section 34 oxidizes the carbon monoxide in the reformed gas to reduce the carbon monoxide concentration in the reformed gas, and converts the carbon monoxide concentration into a fuel gas having a predetermined amount or less.
• the carbon monoxide sensor 40 is provided in a communication pipe 36 that supplies the reformed gas generated in the reforming section 32 to the CO selective oxidizing section 34, and detects the concentration of carbon monoxide in the reformed gas. To detect.
• the blower 38 contains oxygen in the communication pipe 36 via an introduction pipe 39 connected downstream of the carbon monoxide sensor 40 of the communication pipe 36. An oxidizing gas (air in this embodiment) is introduced.
• the control unit 70 controls the operation state of each unit of the fuel reformer 30. Hereinafter, each component of the fuel reformer 30 will be described in more detail.
• the reforming unit 32 receives the supply of methanol from the methanol tank ⁇ 2 and the water from the water tank 14, and performs the steam reforming reaction shown in the above-described equations (4) to (6).
• a reformed gas containing hydrogen and carbon dioxide is generated.
• the conversion reaction of carbon monoxide shown in equation (5) is difficult to be completely performed in practice, so that carbon monoxide as a by-product is contained in the generated reformed gas. Will be mixed by a predetermined amount.
• the concentration of carbon monoxide in the reformed gas depends on the type of catalyst charged in the reforming section 32, the operating temperature of the reforming section 32, and the units of methanol and water supplied to the reforming section 32. It depends on the supply flow rate per unit. In this example, a Cu—Zn catalyst was used as a catalyst to be charged into the reforming section 32.
• This Cu-Zn catalyst is a catalyst made of a metal oxide produced by a well-known coprecipitation method and is formed into a tablet having a diameter of about 3 mm.
• the reforming section 32 is filled with the tablet-shaped Cu—Zn catalyst. Methanol and water are vaporized in an evaporator (not shown) provided upstream of the reforming section 32, and a mixed gas composed of methanol and water is supplied to the reforming section 32 as a raw fuel gas.
• the raw fuel gas introduced into the reforming section 32 comes into contact with the Cu-Zn catalyst, and the reforming reaction proceeds on the Cu-Zn catalyst. Hydrogen and carbon dioxide are generated with the progress of the reforming reaction, and hydrogen-rich reformed gas is supplied to the connecting pipe 36.
• the reforming section 32 Since the reforming reaction carried out in the reforming section 32 is an endothermic reaction as a whole (reaction of the formula (6)), the reforming section 32 is provided with a combustion (not shown) in order to obtain the heat required for the reaction. It has a part.
• This combustion section receives supply of methanol from a methanol tank 12 as fuel for combustion. By controlling the amount of methanol supplied to the combustion section, the operating temperature of the reforming section 32 is controlled in the range of 220 ° C to 300 ° C.
• the reforming unit 32 is connected to the control unit 70, and the control unit 70 controls the supply amount of methanol to the combustion unit and the supply amounts of methanol and water to the reforming unit 32. I have.
• the CO selective oxidizing unit 34 receives the supply of the reformed gas and the oxidizing gas generated in the reforming unit 32 and oxidizes carbon monoxide in the reformed gas in preference to hydrogen. Is a fuel gas with a low carbon monoxide concentration. That is, the CO selective oxidizing section 34 functions as a carbon monoxide concentration reducing section in the fuel reforming apparatus 30.
• FIG. 4 is an explanatory diagram schematically showing the configuration of the CO selective oxidation section 34.
• the CO selective oxidation section 34 is filled with the above-described lithium-added ruthenium catalyst, that is, alumina pellets having lithium and ruthenium supported on the surface, as a carbon monoxide selective oxidation catalyst.
• the reforming gas When the reforming gas is supplied from the reforming unit 32 to the CO selective oxidizing unit 34 through the communication pipe 36, the reforming gas passes through the surface of the above-mentioned ruthenium-doped ruthenium catalyst. The selective oxidation reaction proceeds, and the concentration of carbon monoxide in the reformed gas is reduced. When the reformed gas having a reduced carbon monoxide concentration is discharged from the CO selective oxidation section 34, it is supplied to the fuel cell 20 as a fuel gas.
• the reforming gas is supplied to the CO selective oxidizing unit 34, and the carbon monoxide concentration in the fuel gas obtained by reducing the carbon monoxide concentration depends on the operating temperature of the CO selective oxidizing unit 34, the CO selective oxidizing unit 3 4 It is determined by the concentration of carbon monoxide in the reformed gas supplied to the CO, and the flow rate (space velocity) per unit catalyst volume of the reformed gas supplied to the CO selective oxidation section 34.
• the carbon monoxide sensor 40 is provided in the communication pipe 36 as described above, and detects the concentration of carbon monoxide in the reformed gas supplied to the CO selective oxidation section 34 via the communication pipe 36. It is a sensor to detect.
• the carbon monoxide sensor 40 is connected to the control unit 70, and outputs information on the detected concentration of carbon monoxide in the reformed gas to the control unit 70.
• the blower 38 is a device for supplying air used for oxidizing carbon monoxide to the CO selective oxidizing unit 34, and is connected to the control unit 70. A predetermined amount of air is supplied to the CO selective oxidation unit 34 in response to a drive signal from the control unit 70.
• the control unit 70 inputs information on the concentration of carbon monoxide in the reformed gas supplied to the CO selective oxidation unit 34 from the carbon monoxide sensor 40, and A drive signal is output to the blower 38 based on the information. Therefore, the blower 38 is provided with carbon monoxide in the reformed gas supplied to the CO selective oxidation section 34. An amount of air corresponding to the element concentration can be supplied to the CO selective oxidation section 34.
• the control unit 70 is configured as a logic circuit centered on a microcomputer. Specifically, the control unit 70 executes a predetermined operation according to a preset control program, and the CPU 72 executes various arithmetic processing. ROM 74 pre-stored with control programs and control data necessary for operation, RAM 76 for temporarily reading and writing various data necessary for executing various arithmetic processing by the CPU 72, and carbon monoxide. In addition to inputting detection signals from the sensor 40, etc., and inputting drive signals to the reforming section 32, the CO selective oxidizing section 34, the blower 38, the carbon monoxide sensor 40, etc. in accordance with the calculation results in the CPU 72. It has an output port 78 and so on.
• the CO selective oxidizing unit 34 includes the lithium-added ruthenium catalyst described above as the carbon monoxide selective oxidizing catalyst.
• a gas in which the concentration of carbon monoxide in the reformed gas is sufficiently reduced can be supplied to the fuel cell 20 as a fuel gas.
• Figure 5 shows the performance of reducing the concentration of carbon monoxide in hydrogen rich gas under various temperature conditions for the ruthenium catalyst, which is a conventionally known carbon monoxide selective oxidation catalyst, and the lithium-doped ruthenium catalyst of the present embodiment.
• FIG. 9 is an explanatory diagram showing a result of the comparison.
• the ruthenium catalyst used as a comparative example was obtained by performing only the steps similar to the steps from step S140 to step S170 in the method of manufacturing the lithium-added ruthenium catalyst shown in FIG. It is manufactured by supporting only ruthenium on a plate.
• the supported amount of ruthenium was 0.036 mol Z liter (the number of moles of the supported ruthenium per volume of the alumina pellet).
• the test for examining the performance of the carbon monoxide selective oxidation catalyst shown in FIG. 5 was performed as follows.
• Each of the catalysts is first charged into a reaction vessel having a volume of about 1 Ocm 3 , and the reaction vessel filled with the catalyst is fed from the reforming section 32 of the fuel cell device 10 to the C0 selective oxidizing section 34.
• a model gas having a general composition in the reformed gas supplied to the company was supplied.
• the reformed gas obtained by performing the steam reforming reaction of methanol with the molar ratio [H 20 ] / [C HsOH] of water and methanol at 2 is obtained.
• the humidity of the model gas was adjusted to obtain the same humidified state, and air as an oxidizing agent for carbon monoxide was mixed and introduced into the reaction vessel filled with the catalyst.
• air as an oxidizing agent for carbon monoxide
• the molar ratio of carbon monoxide of the model gas [0 2] / [CO] is the value 3
• An amount of air was mixed into the model gas.
• the gas flow rate when introducing the humidified and air-mixed model gas into the reaction vessel filled with the catalyst was 800 cm 3 min.
• the model gas is introduced into the reaction vessel filled with each of the lithium-added ruthenium catalyst of the present example and the ruthenium catalyst as the comparative example, and the selective oxidation reaction of carbon monoxide is performed in the reaction vessel.
• the concentration of carbon monoxide in the reformed gas discharged from each reaction vessel after the concentration of carbon monoxide was reduced was measured by gas chromatography.
• Such a test for examining the performance of each catalyst for reducing the carbon monoxide concentration was conducted under the respective temperature conditions of 100 ° C, 140 ° C, and 200 ° C for each catalyst.
• the carbon monoxide concentration in the hydrogen-rich gas under any of 100 ° C., 140 ° C., and 200 ° C. was sufficiently reduced.
• the carbon monoxide concentration can be reduced to about the same level as the lithium-added ruthenium catalyst under the temperature conditions of 140 ° C and 200 ° C.
• the catalyst temperature was set at 100 ° C., the performance of reducing the carbon monoxide concentration was significantly inferior to that of the lithium-added ruthenium catalyst.
• the temperature range in which the concentration of carbon monoxide can be sufficiently reduced extends to a lower temperature side than before, and in a wide temperature range from 100 ° C to 200 ° C.
• the concentration of carbon monoxide in the hydrogen rich gas can be sufficiently reduced. Therefore, in the fuel cell device 10 including the CO selective oxidizing unit 34 filled with such a lithium-added ruthenium catalyst, control of the internal temperature of the CO selective oxidizing unit 34 becomes easier, and the entire fuel cell device 10 is controlled. Can be further simplified. That is, in the CO selective oxidizing section 34, the temperature range in which the concentration of carbon monoxide in the hydrogen-rich gas can be sufficiently reduced is broadened to a lower temperature side.
• the temperature of the fuel gas discharged from the CO selective oxidizing unit 34 and the operating temperature of the fuel cell 20 can be made closer, and the fuel gas discharged from the CO selective oxidizing unit 34 can be Prior to supplying the fuel gas to zero, the structure for lowering the temperature of the fuel gas can be further simplified or omitted.
• the lithium-added ruthenium catalyst of this example has sufficient activity even at a high temperature of about 200 ° C., similar to a conventionally known ruthenium catalyst, and therefore, the reformed catalyst discharged from the reforming section 32 is not required.
• the gaseous gas can be directly introduced into the CO selective oxidation section 34 to be subjected to the carbon monoxide selective oxidation reaction. That is, since the reforming section 32 equipped with the Cu—Zn catalyst normally proceeds with the reforming reaction in a temperature range of 250 to 300 ° C., the CO selective oxidizing section The temperature of the reformed gas supplied to 34 becomes about 200 ° C., which allows it to be subjected to a selective oxidation reaction of carbon monoxide.
• the inside is cooled by a method such as circulating cooling water around the CO selective oxidation section 34, so that the internal catalyst temperature is reduced to about 2 as a whole. If the catalyst temperature is controlled so as to be below 0 ° C and the catalyst temperature near the outlet drops to about 10 ° C, the reforming section 32, the CO selective oxidizing section 34 and the fuel cell 20 are connected.
• the entire piping configuration can be simplified.
• the lithium-added ruthenium catalyst of the present embodiment has a wider temperature range in which the concentration of carbon monoxide in hydrogen rich gas can be sufficiently reduced as compared with a conventionally known ruthenium catalyst, the CO selective oxidation unit 34
• the temperature range allowed as the internal catalyst temperature in the catalyst is widened, and the temperature control in the CO selective oxidizing section 34 is facilitated.
• the internal catalyst temperature in the CO selective oxidation section 34 The CO selective oxidizing unit 34 stably reduces the concentration of carbon monoxide even when the size of the load connected to the fuel cell 20 fluctuates due to the widened temperature range allowed as the temperature It becomes possible.
• the amount of reformed gas supplied to the CO selective oxidizing section 34 fluctuates with the fluctuation of the load, and the amount of heat generated by the carbon monoxide selective oxidizing reaction progressing in the CO selective oxidizing section 34 is reduced. Even if the temperature fluctuates and the internal temperature of the CO selective oxidizing section 34 rises and falls, the CO selective oxidizing section 34 maintains a temperature range in which the internal temperature can sufficiently reduce the concentration of carbon monoxide in the hydrogen rich gas. It is possible to continue to generate fuel gas with a sufficiently low carbon monoxide concentration without deviating from the above.
• the use of a lithium-added ruthenium catalyst in which lithium is supported together with ruthenium on alumina pellets has an activity to promote the selective oxidation of carbon monoxide, as compared with the case of using a conventionally known ruthenium catalyst.
• the temperature range in which the temperature was sufficiently high was expanded to the low temperature side, and the above-mentioned effects could be obtained.
• an example in which the same effect as the above-described ruthenium-added ruthenium catalyst can be obtained for a catalyst including a second element other than lithium together with ruthenium will be described.
• a second element exhibiting the effect of further improving the activity of the ruthenium catalyst for promoting the selective oxidation reaction of carbon monoxide as in the case of the above lithium, here, as in the case of lithium, the force belonging to Al metal , Lithium, lithium belonging to alkaline earth metal, and nickel and zinc were used.
• a catalyst including potassium as the second element is referred to as a lithium-added ruthenium catalyst.
• a method for producing a catalyst including the above-described second element together with ruthenium will be described. Both catalysts were produced by the same method as the lithium-added ruthenium catalyst shown in Fig. 1.
• a potassium salt was adsorbed on alumina pellets in a step corresponding to step S110 in FIG. 1, using a potassium acetate aqueous solution instead of the lithium acetate aqueous solution.
• the barium-added ruthenium catalyst uses a barium acetate aqueous solution in the step corresponding to step S110, and the nickel-added ruthenium catalyst also uses a nickel nitrate aqueous solution
• the zinc-added ruthenium catalysts similarly, aqueous solutions of zinc nitrate were used, and the respective salts were adsorbed on alumina pellets.
• a ratio of 0.05 m0 I liter (the number of moles of the supported second element per volume of the alumina pellet) is used.
• a second element was supported on an alumina pellet.
• ruthenium was supported on the alumina pellet at a rate of 0.036 m 0 I / liter (the number of moles of supported ruthenium per volume of the aluminum pellet).
• FIG. 5 shows the results for the ruthenium catalyst. Shown here are the results of tests performed under the same conditions as for the lithium-added ruthenium catalyst described above. As shown in FIG. 5, the ruthenium catalyst to which the second element other than lithium was added was 100 ° C., 140 ° C., and 200 ° C., similarly to the lithium-added ruthenium catalyst. Under any of the above temperature conditions, the concentration of carbon monoxide in the hydrogen-rich gas was sufficiently reduced.
• the temperature range in which the concentration of carbon monoxide can be sufficiently reduced is lower than in the case of using a ruthenium catalyst to which lithium is added. Is further spread to the low temperature side, and the carbon monoxide concentration in the hydrogen rich gas can be sufficiently reduced in a wide temperature range from 100 ° C. to 200 ° C.
• the fuel cell device As in the case of 10, the control of the internal temperature of the CO selective oxidizing section becomes easier, and the configuration of the entire fuel cell device can be further simplified. In other words, since the temperature range in which the concentration of carbon monoxide in the hydrogen-rich gas can be sufficiently reduced has been broadened to lower temperatures, the temperature near the outlet of the CO selective oxidation unit is controlled to be lower than before.
• such a ruthenium catalyst to which the second element is added has sufficient activity even at a high temperature of about 200 ° C., similar to the lithium-added ruthenium catalyst and the conventionally known ruthenium catalyst, so
• the reformed gas discharged from the carbon dioxide section can be directly introduced into the CO selective oxidation section and used for the carbon monoxide selective oxidation reaction. Therefore, in the CO selective oxidizing section, the internal catalyst temperature becomes approximately 200 ° C or less as a whole, such as by circulating cooling water around it, and the catalyst temperature becomes 100 ° C near the outlet.
• the ruthenium catalyst to which the second element is added like the lithium-added ruthenium catalyst, has a temperature range in which the concentration of carbon monoxide in the hydrogen-rich gas can be sufficiently reduced as compared with a conventionally known ruthenium catalyst. Since the temperature is wide, the temperature range allowed as the internal catalyst temperature in the CO selective oxidizing section is widened, and the temperature control in the CO selective oxidizing section is facilitated. As described above, even if the magnitude of the load connected to the fuel cell fluctuates due to the widened temperature range allowed as the internal catalyst temperature in the CO selective oxidation section, as described above, The selective oxidation unit can stably reduce the concentration of carbon monoxide.
• potassium acetate is used for the potassium-added ruthenium catalyst
• barium acetate is used for the barium-added ruthenium catalyst
• nickel is used.
• Nickel nitrate was used for the added ruthenium catalyst
• zinc nitrate was used for the zinc-added ruthenium catalyst, but other types of compounds may be used. It may be appropriately selected from other nitrates, acetates, chlorides, sulfides and the like.
• the raw material for supporting ruthenium on the carrier is not limited to ruthenium chloride, and other types of ruthenium compounds may be used as in the case of the aforementioned lithium-added ruthenium catalyst.
• the applicant of the present application has already made a platinum-ruthenium alloy catalyst.
• This platinum-ruthenium alloy catalyst also has an effect that the activity of promoting the selective oxidation reaction of carbon monoxide can be remarkably improved as compared with a conventionally known ruthenium catalyst (a catalyst containing no other element). are doing.
• the ruthenium catalyst to which the above-described second element including lithium is added has an even more excellent effect as compared with such a platinum-ruthenium alloy catalyst.
• the above-described reverse shift reaction proceeds together with the selective oxidation reaction of carbon monoxide, so that an obstacle in sufficiently reducing the concentration of carbon monoxide in the reformed gas.
• the ruthenium catalyst to which lithium and other elements are added has the methanation activity of methanizing carbon monoxide, similar to a conventionally known ruthenium catalyst.
• the carbon monoxide generated by the reverse shift reaction can be methanated to sufficiently reduce the concentration of carbon monoxide in the reformed gas.
• the following shows a formula representing the methanation reaction of carbon monoxide.
• the activity of promoting the reaction of methanizing carbon monoxide shown in equation (9) is the activity inherent in ruthenium catalysts, but the ruthenium catalyst to which the above-mentioned secondary elements such as lithium are added is added. Thus, even if the second element is added, the activity for promoting such a methanation reaction is sufficiently maintained. Since the reverse shift reaction is an endothermic reaction, the effect of promoting the methanation reaction shown in Eq. (9) is remarkable especially in the region where the temperature of the catalyst filled in the CO selective oxidation unit is higher. can get.
• the above-mentioned platinum-ruthenium alloy catalyst further activates the above-mentioned reverse shift reaction, and thus has an activity to promote the methanation reaction similarly to the conventionally known ruthenium catalyst.
• the methanation reaction may impair the effect of further reducing the concentration of carbon monoxide in the reformed gas.
• the ruthenium catalyst to which the above-mentioned second element such as lithium is added can sufficiently consume carbon monoxide generated by the reverse shift reaction by the methanation reaction, and can be compared with the platinum-ruthenium alloy catalyst.
• the concentration of carbon monoxide in the reformed gas can be effectively reduced.
• the above-mentioned second elements such as lithium are more expensive than platinum. Therefore, by using these second elements, the cost of the carbon monoxide selective oxidation catalyst can be reduced as compared with the case of producing a platinum-ruthenium alloy catalyst.
• the second element including lithium which is an element to be added together with ruthenium, is supported at a rate of 0.05 mo IZ liter. May be selected, and the amount of ruthenium to be supported is set to be 0.036 mol Z liter. However, a different amount of ruthenium may be selected. That is, in the above-described embodiment, the molar ratio between the second element and ruthenium is set to the value 0.3, but may be different. If the proportion of the second element is too large, the surface of the ruthenium present as particles on the carrier is covered by the second element, and the specific surface area of ruthenium decreases.
• the processing capacity of the C0 selective oxidation unit equipped with the carbon monoxide selective oxidation catalyst that is, the maximum space velocity at which the concentration of carbon monoxide in the supplied hydrogen rich gas can be sufficiently reduced is reduced.
• the molar ratio of the second element to ruthenium can be reduced as long as the capacity to reduce the concentration of carbon monoxide in the hydrogen rich gas supplied to the CO selective oxidizing unit is sufficiently ensured. The value can exceed 0.14.
• the proportion of the second element is too small, the effect of improving the activity of promoting the selective oxidation reaction of carbon monoxide may be insufficient.However, the second element is uniformly dispersed in the vicinity of the ruthenium particles, If the effect of adding the second element is sufficiently obtained, the molar ratio between the second element and ruthenium may be a value lower than 0.14.
• the molar ratio of the second element and ruthenium that is, the supported amount of the second element and ruthenium is determined by the ratio of the amount of the aqueous solution of the salt containing the second element to the alumina pellet in the step of producing the catalyst. By changing the ratio of the amount of the ruthenium salt aqueous solution to the amount of the alumina pellet, it can be adjusted to an arbitrary value.
• ruthenium is loaded on the alumina pellet first, and then ruthenium is supported on the alumina pellet.
• the surface of ruthenium is covered with the second element, and the ratio of ruthenium is reduced. If the surface area is reduced and the above-mentioned inconvenience does not occur, the second element may be supported after supporting ruthenium.
• ruthenium and the second element may be simultaneously supported on alumina pellets.
• an alloying treatment of ruthenium and the second element may be further performed.
• the microscopic position of the ruthenium and the second element is closer to each other, and when working as a catalyst for selective oxidation of carbon monoxide, the interaction between the ruthenium and the second element is reduced. The effect can be expected to be more active.
• the production of the ruthenium catalyst to which the second element has been added as described above may be carried out by a production method other than the above, as long as a sufficient catalytic activity can be obtained.
• the second element may be supported on the alumina pellet as described above, or may be added to the alumina pellet in advance in the process of producing the alumina pellet. That is, the catalyst may be produced so that the second element is present in the vicinity of ruthenium to the extent that the effect of promoting the selective oxidation reaction of carbon monoxide can be improved.
• a honeycomb may be used instead of the alumina pellet.
• a metal catalyst prepared by pulverizing a catalyst (a catalyst in which ruthenium and a second element are supported on alumina pellets) manufactured in the same manner as in the above-described embodiment is coated on a metal honeycomb.
• a catalyst-supporting honeycomb or to coat the honeycomb with alumina in advance, and to carry out a treatment for supporting ruthenium and the second element on the same as in the case of using the alumina pellet described above.
• a catalyst-carrying honeycomb can be manufactured.
• alumina is used as a carrier for supporting a catalytic metal having an activity of promoting a selective oxidation reaction of carbon monoxide.
• the carbon monoxide concentration reducing device, the carbon monoxide concentration reducing method, and the carbon monoxide selective oxidation catalyst according to the present invention are useful in a fuel gas supply device that supplies hydrogen rich gas to a fuel cell. It can be used in the field of manufacturing electric vehicles using a fuel cell as a driving power source.

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• 1997
  • 1997-09-26 JP JP9279694A patent/JPH11102719A/ja active Pending
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